CN103508418B - Go into operation gas heating system and heating means in water vapour process for making hydrogen - Google Patents
Go into operation gas heating system and heating means in water vapour process for making hydrogen Download PDFInfo
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- CN103508418B CN103508418B CN201210206409.XA CN201210206409A CN103508418B CN 103508418 B CN103508418 B CN 103508418B CN 201210206409 A CN201210206409 A CN 201210206409A CN 103508418 B CN103508418 B CN 103508418B
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Abstract
The invention provides go into operation gas heating system and the method in water vapour process for making hydrogen, this system comprises unstripped gas and divides flow container, middle change gas raw material interchanger and heat exchange cooling unit.Heat exchange cooling unit comprises heat exchanging segment and cooling section, and heat exchanging segment comprises middle change gas raw material interchanger, and its tube-side inlet is connected with Medium Pressure Steam Pipeline, and the outlet of its tube side is connected with low-pressure steam pipe network by vapour line; The described gas that goes into operation enters system from the gas inlet mouth that goes into operation, through unstripped gas divide flow container laggard enter middle change gas raw material heat exchanger shell pass entrance, after shell-side outlet goes out, enter hydrogenator; Export out through cooling section from hydrogenator afterwards, return unstripped gas and divide flow container, form the circulation loop heating the gas system that goes into operation.The present invention's gas heating system that goes into operation successively realizes heating and to go into operation gas and prepare hydrogen two kinds of operating mode and switch, and need not arrange the system of going into operation specially, reduce investment outlay cost and occupation area of equipment, plant factor significantly improves.
Description
Technical field
The present invention relates to hydrocarbon steam conversion technique hydrogen preparation field, particularly relate to go into operation gas heating system and heating means in the sulfidation in water vapour process for making hydrogen.
Background technology
Adopt the device for producing hydrogen of steam reforming technique to use Sweet natural gas, refinery gas, coking dry gas, light oil etc. are raw material, have the different flow arrangements that goes into operation for different material when going into operation.Natural gas, because is simple for institute's sulfur-type, does not therefore need to carry out prevulcanized to hydrogenation catalyst specially.If but use the coking dry gas of sulfur-bearing kenel complexity or light oil to be raw material, when going into operation, the sulfuration of hydrogenation catalyst must be carried out.Therefore device for producing hydrogen is provided with is separately hydrogenation catalyst sulfuration and the flow process that goes into operation of establishing, and this cover flow process is except compressor continues when normal running to use, and other facility does not re-use.It is that hydrogenation catalyst heats up and sulfuration that early stage device for producing hydrogen is provided with the special process furnace that goes into operation, and does not re-use after going into operation.Rate of utilization is low, causes the wasting of resources, needs consume fuel as thermal source simultaneously, causes a large amount of energy consumption.Develop into later stage a lot of device for producing hydrogen all to eliminate go into operation process furnace then the use well heater that goes into operation and provide heating for hydrogenation catalyst sulfuration.But face too go into operation terminate after go into operation well heater, the water cooler that goes into operation, go into operation that point flow container no longer uses, plant factor is low, problem that waste is invested.
As shown in Figure 1, the go into operation flow process of heat air of existing heating is as follows: the gas that goes into operation (nitrogen, hydrogen) divides flow container 7 from the incoming stock gas of pipe 1, feed gas compressor 8 is entered after separatory, through the tube side 3 of the well heater 9 that goes into operation after boosting, middle pressure steam enters from the shell side 15 of the well heater that goes into operation the heater heats that goes into operation and to go into operation gas.
Such scheme reaches hydrogenator temperature in by variable valve 13 steam regulation amount, returns the entrance that unstripped gas divides flow container 7 from hydrogenator 10 gas that goes into operation out after the water cooler 11 that goes into operation cools.After getting through this circulation, can to heat up according to catalyst vulcanization curve, sulfuration, until sulfuration terminates.
Chinese patent CN1051896 provides a kind of sulphur resisting and low temp conversing processes and reactor.This patented technology adopts raw gas to change carbon monoxide wherein into hydrogen through preheating, sulfur-resisting transformation; belong to sulfur-resisting transformation process during normal production; and the present invention is the sulfuration process scheme by improving hydrogenation catalyst; thus eliminating special vulcanizing deice, the object of protection of the two is all not identical with goal of the invention.
Summary of the invention
To go into operation the defects such as plant factor in air-flow journey is low, power consumption is larger to solve heating of the prior art, the present invention have studied a kind of system and method heating the gas that goes into operation in water vapour hydrogen manufacturing goes into operation, the flow process that the present invention utilizes device normally to run, by suitable combination and linking, the gas that goes into operation before realizing hydrogenation catalyst presulfurizing heats, and these devices can continue to use in follow-up Hydrogen making technological process.
An object of the present invention is to provide the heating system of the gas that goes into operation in a kind of water vapour process for making hydrogen.The described gas heating system that goes into operation is as follows:
The gas heating system that goes into operation in water vapour process for making hydrogen, comprises the gas inlet mouth 1 that goes into operation, the unstripped gas that connect successively and divides flow container 2 and heat exchange cooling unit.
Heat exchange cooling unit comprises heat exchanging segment and cooling section, wherein heat exchanging segment comprises middle change gas raw material interchanger 3, the tube-side inlet of middle change gas raw material interchanger 3 is connected with Medium Pressure Steam Pipeline 6, the tube side outlet of middle change gas raw material interchanger 3 is connected with vapour line 7, and vapour line 7 is connected with low-pressure steam pipe network.Achieve in utilization and become gas raw material interchanger 3 to replace in prior art the conventional well heater that goes into operation, utilize middle pressure steam to heat and go into operation gas to complete the sulfuration to hydrogenation catalyst.
The gas that goes into operation enters system from the gas inlet mouth 1 that goes into operation, and divides after flow container 2 and enters middle change gas raw material interchanger 3 shell side inlet, after shell-side outlet goes out, enter hydrogenator 4 through unstripped gas; Through overcooling section after going out from the outlet of hydrogenator 4, return unstripped gas and divide flow container 2, form the circulation loop heating the gas system that goes into operation.
Specifically:
In order to use the equipment in normal Hydrogen making technological process technique to replace the special heating-cooling apparatus that goes into operation, cooling section comprises oiler feed interchanger 11, de-mineralized water interchanger 12, air cooler 13 and water cooler 14 successively; The tube-side inlet of oiler feed interchanger 11 is connected with the outlet line of hydrogenator 4, and the tube side outlet of water cooler 14 divides the source line of flow container 2 to be connected with unstripped gas.After the tube side of oiler feed interchanger (11), de-mineralized water interchanger (12), air cooler (13) and water cooler (14), enter unstripped gas from hydrogenator (4) gas that goes into operation out and divide flow container (2).Realize utilizing the oiler feed interchanger 11 in normal Hydrogen making technological process, de-mineralized water interchanger 12, air cooler 13 and water cooler 14 to replace the water cooler that goes into operation conventional in prior art.
In concrete enforcement, unstripped gas divides between the shell side inlet of flow container 2 and middle change gas raw material interchanger 3 and is provided with feed gas compressor 16.The gas that goes into operation divides after flow container 2 and feed gas compressor 16 through unstripped gas and enters middle change gas raw material interchanger 3 shell side inlet again.
The first blind plate 5 is provided with between the tube-side inlet of middle change gas raw material interchanger 3 and Medium Pressure Steam Pipeline 6; Connection line between vapour line 7 and low-pressure steam pipe network is provided with variable valve 17, and the vapour line 7 between the tube side outlet of middle change gas raw material interchanger 3 and variable valve 17 is provided with the second blind plate 8.
The outlet of hydrogenator 4 and the connection line of cooling section are provided with the 3rd blind plate 10.
Cooling section outlet and unstripped gas divide the pipeline between flow container 2 entrance to be provided with the 7th blind plate 23.
The outlet of hydrogenator 4 is drawn pipeline and is connected with desulphurization reactor 18, converter 19 and middle change reactor 20 pipeline successively, the outlet of middle change reactor 20 is connected with the tube-side inlet pipeline of middle change gas raw material interchanger 3, hydrogenator 4 connection line exported between desulphurization reactor 18 entrance is provided with the 5th blind plate 21, and middle change reactor 20 exports and be provided with the 6th blind plate 22 between middle change gas raw material interchanger 3 tube-side inlet.
The tube side outlet of middle change gas raw material interchanger (3) is drawn pipeline and is connected with cooling section, and this pipeline is provided with the 4th blind plate (15); Pipeline between cooling section outlet and follow-up hydrogen producer entrance is provided with the 8th blind plate 24.
When going into operation, open described the first blind plate 5, second blind plate 8, the 3rd blind plate 10 and the 7th blind plate 23, the 4th blind plate 15 described in closedown, the 5th blind plate 21, the 6th blind plate 22 and the 8th blind plate 24.Going into operation in gas heat-processed, the 4th blind plate 15 seals the connection of middle change gas raw material interchanger 3 and cooling section, and the 5th blind plate 21 seals the connection of go into operation gas and desulphurization reactor 18.The tube side becoming gas raw material interchanger 3 in middle pressure steam warp advances into low-pressure steam pipe network from the 4th blind plate 15, after the gas that goes into operation exports out from hydrogenator 4, after the 4th blind plate 15, enters cooling section.
After the end that goes into operation, by extremely blind to the first blind plate 5, second blind plate 8, the 3rd blind plate 10 and the 7th blind plate 23, open the 4th blind plate 15, the 5th blind plate 21, the 6th blind plate 22 and the 8th blind plate 24, the middle change gas formed in normal hydrogen manufacturing link enters the passage of middle change gas raw material interchanger 3 tube side, makes native system possess the function of normal hydrogen manufacturing.
Two of object of the present invention is to provide the heating means of the gas that goes into operation in a kind of water vapour process for making hydrogen.The described gas heating means that go into operation, it is the tube side becoming gas raw material interchanger 3 in being introduced by middle pressure steam, the gas that goes into operation through in become the shell side of gas raw material interchanger 3, utilize middle pressure steam to heat the gas that goes into operation, make to go into operation temperature required when to reach sulfuration when gas enters hydrogenator 4; The gas that goes into operation leaving hydrogenator 4 through cooling and after separatory, then through in become gas raw material interchanger 3 steam heating enter hydrogenator 4, complete the gas circulation that goes into operation.
Particularly, utilize variable valve 17 to control amount that middle pressure steam is incorporated to low-pressure steam pipe network, thus in controlling, become the middle pressure steam content in gas raw material interchanger 3, realize the temperature degree that goes into operation entering hydrogenator 4 in sulfidation.
The gas that goes into operation leaving hydrogenator 4 enters the oiler feed interchanger 11 of cooling section, de-mineralized water interchanger 12, air cooler 13, water cooler 14 cool, and after unstripped gas divides flow container 2 to carry out separatory, enter the gas circulation that goes into operation again.
The gas heating means that go into operation of the present invention comprise following concrete steps:
Step one:
When going into operation, open the first blind plate 5, second blind plate 8, the 3rd blind plate 10 and the 7th blind plate 23, close the 4th blind plate the 15, five blind plate 21, the 6th blind plate 22 and the 8th blind plate 24.The gas inlet mouth 1 that goes into operation passes into the gas that goes into operation (nitrogen, hydrogen), and the incoming stock gas of the gas that goes into operation divides flow container 2, after buffering and separatory, leaves and enters feed gas compressor 16 boost from top.
Step 2:
The gas that goes into operation after boosting enters the shell side of middle change gas raw material interchanger 3; Meanwhile, middle pressure steam enters the tube side of middle change gas raw material interchanger 3 by described Medium Pressure Steam Pipeline 6, by the gas that goes into operation in middle pressure steam heating shell side, enters hydrogenator 4 by the shell side gas that goes into operation out;
The middle pressure steam content controlling to enter middle change gas raw material interchanger 3 tube side by outlet regulating valve 17 controls to go into operation the temperature of gas; Particularly, open variable valve 17, middle pressure steam is introduced low-pressure steam pipe network by the tube side of middle change gas raw material interchanger 3 through vapour line 7, the temperature realizing entering the gas that goes into operation of hydrogenator 4 by regulating variable valve 17 controls, according to the intensification of hydrogenation catalyst, curing temperature curve, sulfuration can be realized according to the requirement of catalyzer;
Step 3:
Cooled through oiler feed interchanger 11, de-mineralized water interchanger 12, air cooler 13 and water cooler 14 successively by hydrogenator 4 gas that goes into operation out, the gas that goes into operation leaving water cooler 14 turns back to unstripped gas and divides flow container 2 entrance to carry out separatory, forms the circulation of the gas that goes into operation;
Step 4:
After terminating when going into operation, close the first blind plate 5, blind dead Medium Pressure Steam Pipeline 6, closes the second blind plate 8 simultaneously, cuts off the vapour line into and out of middle change gas feed heater 3 tube side, close the 3rd blind plate 10 and the 7th blind plate 23, open the 4th blind plate 15, 5th blind plate 21, 6th blind plate 22 and the 8th blind plate 24, revert to normal running flow process, namely be make the gas that goes into operation in hydrogenator 4 through desulphurization reactor 18, after converter 19 and middle change reactor 20, the tube side of gas raw material interchanger 3 is become in warp, again through boiler cold-water heat exchanger 11, de-mineralized water interchanger 12, the tube side of air cooler 13 and water cooler 14 cools, 7th blind plate 23 seals water cooler 14 and unstripped gas and divides pipeline between flow container 2 entrance, change gas is made to transfer in existing follow-up hydrogen producer flow process, complete hydrogen manufacturing.
The present invention is the middle change gas heating and cooling part utilizing existing procedure, realizes going into operation the heating and cooling of circulation gas.Middle change gas raw material interchanger 3 in normal flow is arranged into reclaiming reaction heat.Core of the present invention utilizes existing middle change gas raw material interchanger 3 to heat; Utilize oiler feed interchanger 11, de-mineralized water interchanger 12, air cooler 13, water cooler 14 and unstripped gas to divide flow container 2 to cool cooling and separatory that separatory flow process completes the circulation gas that goes into operation.Ingenious make use of now of the present invention becomes gas cooling process, cools the circulation gas that goes into operation.
The beneficial effect that the present invention brings is as follows:
The present invention becomes gas raw material interchanger and substitutes the gas heating installation that goes into operation to the gas heating that goes into operation in utilizing, enable hydrogenation catalyst elevated temperature cure; Utilize the middle change air cooling in existing Hydrogen making technological process but, separatory facility realizes the go into operation cooling of gas and separatory circulation, and possess the hydrogen manufacturing function identical with existing device for producing hydrogen simultaneously, the system of going into operation need not be set specially for hydrogenation catalyst sulfuration, greatly save the floor space of cost of investment and equipment, the utilization ratio of equipment significantly improves.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the gas heating that goes into operation of prior art 1;
Fig. 2 is the process flow sheet of the gas heating system that goes into operation in water vapour process for making hydrogen of the present invention;
Detailed description of main elements:
1-goes into operation gas inlet mouth; 2-unstripped gas divides flow container; Gas raw material interchanger is become in 3-;
4-hydrogenator; 5-first blind plate; 6-Medium Pressure Steam Pipeline; 7-vapour line;
8-second blind plate; 10-the 3rd blind plate; 11-oiler feed interchanger; 12-de-mineralized water interchanger;
13-air cooler; 14-water cooler; 15-the 4th blind plate; 16-feed gas compressor; 17-variable valve;
18-desulphurization reactor; 19-converter; Reactor is become in 20-; 21-the 5th blind plate;
22-the 6th blind plate; 23-the 7th blind plate; 24-the 8th blind plate.
Be described in more detail the present invention below in conjunction with the drawings and specific embodiments, protection scope of the present invention is not limited to following embodiment.
Embodiment
As shown in Figure 2, the gas heating system that goes into operation in water vapour process for making hydrogen, comprise the gas inlet mouth 1 that goes into operation, the unstripped gas that connect successively and divide flow container 2, feed gas compressor 16, middle change gas raw material interchanger 3, and oiler feed interchanger 11, de-mineralized water interchanger 12, air cooler 13 and the water cooler 14 after hydrogenator 4.
Water cooler 14 exports and unstripped gas divides the pipeline between flow container 2 entrance to be provided with the 7th blind plate 23, and water cooler 14 pipeline exported between follow-up hydrogen producer entrance is provided with the 8th blind plate 24.
The tube-side inlet of middle change gas raw material interchanger 3 is connected with the Medium Pressure Steam Pipeline 6 of band first blind plate 5, and the tube side outlet of middle change gas raw material interchanger 3 is connected with vapour line 7, vapour line 7 is provided with successively the second blind plate 8 and outlet regulating valve 17.The outlet of hydrogenator 4 and the connection line of cooling section are provided with the 3rd blind plate 10.The outlet of hydrogenator 4 is drawn pipeline and is connected with desulphurization reactor 18, converter 19 and middle change reactor 20 pipeline successively, hydrogenator 4 exports and be provided with the 5th blind plate 21 between desulphurization reactor 18, the outlet of middle change reactor 20 is connected with the tube-side inlet pipeline of middle change gas raw material interchanger 3, and this pipeline is provided with the 6th blind plate 22; The tube side outlet of middle change gas raw material interchanger 3 is drawn pipeline and is connected with cooling section, and this pipeline is provided with the 4th blind plate 15.
The outlet of hydrogenator 4, after oiler feed interchanger 11, de-mineralized water interchanger 12, air cooler 13 and water cooler 14, divides flow container 2 to be connected with unstripped gas, forms the circulation loop of the gas that goes into operation.
Wherein, the tube-side inlet of oiler feed interchanger 11 is connected with the outlet line of hydrogenator 4, and the tube side outlet of water cooler 14 divides the source line of flow container 2 to be connected with unstripped gas.
The concrete gas heating means that go into operation, comprise the steps:
Step one:
Open the first blind plate 5, second blind plate 8, the 3rd blind plate 10 and the 7th blind plate 23, close the 4th blind plate 15, the 5th blind plate 21, the 6th blind plate 22 and the 8th blind plate 24.The gas inlet mouth 1 that goes into operation passes into the gas that goes into operation, and the incoming stock gas of the gas that goes into operation divides flow container 2, after buffering and separatory, leaves and enters feed compressor 16 boost from top.
Step 2:
The gas that goes into operation after boosting enters the shell side of middle change gas raw material interchanger 3, simultaneously, middle pressure steam enters the tube side of middle change gas raw material interchanger 3 by Medium Pressure Steam Pipeline 6, and by the gas that goes into operation in middle pressure steam heating shell side, the shell side gas that goes into operation out enters hydrogenator 4.The middle pressure steam content controlling to enter middle change gas raw material interchanger 3 tube side by outlet regulating valve 17 controls to enter the temperature of the gas that goes into operation of hydrogenator 4, according to the intensification of hydrogenation catalyst, curing temperature curve, sulfuration can be realized according to the requirement of catalyzer.
Step 3:
Cooled through oiler feed interchanger 11, de-mineralized water interchanger 12, air cooler 13 and water cooler 14 successively by hydrogenator 4 gas that goes into operation out, the gas that goes into operation leaving water cooler 14 turns back to unstripped gas and divides flow container 2 entrance, forms the circulation of the gas that goes into operation.
Step 4:
After terminating when going into operation, blind dead first blind plate 5, closes the second blind plate 8, the 3rd blind plate 10 and the 7th blind plate 23 simultaneously; Open the 4th blind plate 15, the 5th blind plate 21, the 6th blind plate 22 and the 8th blind plate 24, make the tube side becoming gas raw material interchanger 3 in the warp of the gas in hydrogenator 4, transfer in the follow-up flow sheet equipment of existing process for making hydrogen, complete hydrogen manufacturing.Be and make the gas in hydrogenator 4 after desulphurization reactor 18, converter 19 and middle change reactor 20, the tube side of gas raw material interchanger 3 is become in warp, tube side again through boiler cold-water heat exchanger 11, de-mineralized water interchanger 12, air cooler 13 and water cooler 14 cools, then transfer in the follow-up flow sheet equipment of existing process for making hydrogen through the 8th blind plate 24, complete hydrogen manufacturing.
Claims (1)
1. the heating means of the gas heating system that goes into operation in a water vapour process for making hydrogen, the gas heating system that goes into operation in wherein said water vapour process for making hydrogen, comprise the gas inlet mouth (1) that goes into operation, the unstripped gas that connect successively and divide flow container (2) and heat exchange cooling unit
Described heat exchange cooling unit comprises heat exchanging segment and cooling section, wherein said heat exchanging segment comprises middle change gas raw material interchanger (3), the tube-side inlet of described middle change gas raw material interchanger (3) is connected with Medium Pressure Steam Pipeline (6), the tube side outlet of described middle change gas raw material interchanger (3) is connected with vapour line (7), and described vapour line (7) is connected with low pressure steam pipe webmaster line;
Described go into operation gas through described in the gas inlet mouth (1) that goes into operation enter system, divide after flow container (2) through described unstripped gas and enter described middle change gas raw material interchanger (3) shell side inlet, after shell-side outlet goes out, enter hydrogenator (4); Export out through described cooling section from described hydrogenator (4) afterwards, return described unstripped gas and divide flow container (2), form the circulation loop heating the gas system that goes into operation;
The first blind plate (5) is provided with between the tube-side inlet of described middle change gas raw material interchanger (3) and Medium Pressure Steam Pipeline (6);
Connection line between described vapour line (7) and low-pressure steam pipe network is provided with variable valve (17); Vapour line (7) between the tube side outlet of described middle change gas raw material interchanger (3) and described variable valve (17) is provided with the second blind plate (8);
The outlet of described hydrogenator (4) and the connection line of described cooling section are provided with the 3rd blind plate (10);
Described cooling section outlet and described unstripped gas divide the pipeline between flow container (2) entrance to be provided with the 7th blind plate (23);
The outlet of described hydrogenator (4) draw pipeline successively with desulphurization reactor (18), converter (19) and middle change reactor (20) pipeline connect, the outlet of described middle change reactor (20) is connected with the tube-side inlet pipeline of described middle change gas raw material interchanger (3), connection line between wherein said hydrogenator (4) outlet and desulphurization reactor (18) entrance is provided with the 5th blind plate (21), the 6th blind plate (22) is provided with between described middle change reactor (20) outlet and middle change gas raw material interchanger (3) tube-side inlet,
The tube side outlet of described middle change gas raw material interchanger (3) is drawn pipeline and is connected with cooling section, and this pipeline is provided with the 4th blind plate (15); Pipeline between described cooling section outlet and follow-up hydrogen producer entrance is provided with the 8th blind plate (24);
Described cooling section comprises oiler feed interchanger (11), de-mineralized water interchanger (12), air cooler (13) and water cooler (14) successively;
The tube-side inlet of described oiler feed interchanger (11) is connected with the outlet line of described hydrogenator (4), and the tube side outlet of described water cooler (14) divides the source line of flow container (2) to be connected with described unstripped gas;
After the tube side of described oiler feed interchanger (11), de-mineralized water interchanger (12), air cooler (13) and water cooler (14), enter described unstripped gas from described hydrogenator (4) out the gas that goes into operation and divide flow container (2);
Described unstripped gas divides the pipeline between the shell side inlet of the outlet of flow container (2) and described middle change gas raw material interchanger (3) to be provided with feed gas compressor (16);
The described gas that goes into operation divides after flow container (2) and described feed gas compressor (16) through described unstripped gas and enters described middle change gas raw material interchanger (3) shell side inlet again;
It is characterized in that, comprise the following steps:
Step one:
When going into operation, open described the first blind plate (5), the second blind plate (8), the 3rd blind plate (10) and the 7th blind plate (23), the 4th blind plate (15) described in closedown, the 5th blind plate (21), the 6th blind plate (22) and the 8th blind plate (24); The described gas inlet mouth (1) that goes into operation passes into the gas that goes into operation, and the gas that goes into operation enters described unstripped gas and divides flow container (2), after buffering and separatory, leaves and enters feed gas compressor (16) boost from top;
Step 2:
The gas that goes into operation after boosting enters the shell side of described middle change gas raw material interchanger (3), simultaneously, middle pressure steam enters the tube side of described middle change gas raw material interchanger (3) by described Medium Pressure Steam Pipeline (6), by the gas that goes into operation in middle pressure steam heating shell side, the gas that goes into operation after heating enters described hydrogenator (4); The middle pressure steam content controlling to enter middle change gas raw material interchanger (3) tube side by outlet regulating valve (17) controls the temperature of the gas that goes into operation entering hydrogenator (4);
Step 3:
Cooled through the tube side of described oiler feed interchanger (11), de-mineralized water interchanger (12), air cooler (13) and water cooler (14) successively by described hydrogenator (4) gas that goes into operation out, the gas that goes into operation leaving described water cooler (14) turns back to described unstripped gas and divides flow container (2) entrance to carry out separatory, forms the circulation of the gas that goes into operation;
Step 4:
Go into operation after terminating, close described first blind plate (5), the second blind plate (8), the 3rd blind plate (10) and the 7th blind plate (23), open described 4th blind plate (15), the 5th blind plate (21), the 6th blind plate (22) and the 8th blind plate (24), start normal hydrogen manufacturing operating process.
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| CN201210206409.XA CN103508418B (en) | 2012-06-18 | 2012-06-18 | Go into operation gas heating system and heating means in water vapour process for making hydrogen |
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| CN201210206409.XA CN103508418B (en) | 2012-06-18 | 2012-06-18 | Go into operation gas heating system and heating means in water vapour process for making hydrogen |
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| CN103508418B true CN103508418B (en) | 2015-08-12 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104555918A (en) * | 2014-12-31 | 2015-04-29 | 贵州天福化工有限责任公司 | Method and system for recycling high-temperature steam |
| CN106890568A (en) * | 2017-04-13 | 2017-06-27 | 西安热工研究院有限公司 | A kind of carbonyl sulfide hydrolysis device and its driving technique |
| CN107998689B (en) * | 2017-12-04 | 2019-12-17 | 大连理工大学 | Removing CO in the medium-to-variable gas acidic condensate2And O2Heat integrated rectification process |
| CN109701454B (en) * | 2019-01-28 | 2024-02-13 | 安庆市泰发能源科技有限公司 | Butane dehydrogenation start-up circulation heating device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1075740A (en) * | 1992-10-27 | 1993-09-01 | 中国石油化工总公司 | Oil refinery dry gas and the charging of petroleum naphtha mixed phase are produced hydrogen, methane, carbon monoxide, the method for carbonic acid gas from hydrofining |
| US7060118B1 (en) * | 1998-07-21 | 2006-06-13 | Haldor Topse A/S | Synthesis gas production by steam reforming |
| CN102219184A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Process for preheating raw material of hydrogen production device |
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2012
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1075740A (en) * | 1992-10-27 | 1993-09-01 | 中国石油化工总公司 | Oil refinery dry gas and the charging of petroleum naphtha mixed phase are produced hydrogen, methane, carbon monoxide, the method for carbonic acid gas from hydrofining |
| US7060118B1 (en) * | 1998-07-21 | 2006-06-13 | Haldor Topse A/S | Synthesis gas production by steam reforming |
| CN102219184A (en) * | 2010-04-13 | 2011-10-19 | 中国石油化工集团公司 | Process for preheating raw material of hydrogen production device |
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